Processes of refining and purifying fats and higher fatty acids



Patented Oct. 6, 1953 moessss s omssw e FATS AND HIGHER FA" Newii'k, TY.

. Th sen ment et s e a Pro e of refining and purifyina fats, fatty acids anddrivv fv U Q This application is a continuation-in-partof application elN 71 r d; 2??mb 1946, now abandon d, and entitled fBroce'ssesfipf Refining, ur y n enfl li d' q eeefiea Fatty Acids and Waigesffvvhich isa continuationin-part of U. S. patent applicationfierialiflo. 505,254,filed October (i, 1 -9 1f.',vghich hasmatured i o P t -2. 09 ent tled .Bme i s 9 Refining, Purifying, and Hydrogenating Fats. atty Acids and Waxesfi 4 a It is an object of the present invention to provide a new process for refining and purifying fats, fatty acids and derivatives thereof by simplified treatment thereof. i V

It is a further objectdt the prejs'entiinvention to provide processes for clarification, partial heutralization, removal otoil-sol'uble metal soa'psimproving the bleachability of, and hydrogenation of fats, fatty acids and derivatives thereon Another object "of the present invention is to provide a process for refining and-pnrifyingof fats, fatty acids and derivatives thereof which yields very light colored products which contain only traces of impurities. V J a It is a still further object; oi thegpifes'ent invention to provide a process of removingmetal soaps, i. e. nickel and copper soaps, colloidal metal residues and also iron traces from purified, relatively protein free, 'fats, fatty acids and derivatives thereof. a I

With the above objects in view the present invention mainly consists in tratingfats, fatty acids and derivatives thereof with a substance adapted to precipitate "contained lnipurities particularly of the protein "type and separating the purified products from the sludge "containing these impurities.

Freshly rendered fats andfatty acids of vegetable and animal origin including marine oils, sperm oils, glycerideoils, and componentsof these oils are usually cloudy in appearancebecauseoi fines i. e. proteinaceous matter. This protein matter, finesfiar'e still present in emulsion form and are very difiicult, in fact almost impossible to precipitate by gravity or centrifugation and cannot be filtered out. W a I a 1 Purification of these substances involves a; great number of difficulties and separate operations. The present invention provides a process which may be utilized for the purification of these substances in a simplified operation or aseries ot simplified operations in. the case where an extremely pure productis desired.

21615158. (01. ante.)

rm yitwas necessaryim order to; purify a fat *such as 'tallow to submitthe freshly rendered substance tohafseriesjof washingand settlin Oberations to, make a :partial clarification and filtratiOlSizPOSSible or [complete neutralization was necessary to removeimost of then etal soaps.

The present invention provides a process which greatly improves eachpf these individual urifications and which iniactcan be simply,used to purifythe fat andpartially neutralize it all in one operation with-lessimpuritiesleft.

In accordance with the preierred embodiment of the present inventiQmIatsanetreated with a lignin which has been made water soluble by reaction. with an 5 alkali metal compound such as sodium hydroxide or-drysodium phosphate. "It is also possible to usean "aqueous agent containing lignin and'analkali. -In either case it ispreferable to. use a highly purified lignin such as Rimco 957.

Though the present invention may be carried out in one operation or in a series of operations the-substance. of ytheinvention is the use of lignin, preferably in highly purified form, along with an alkali, "theifatior faittyiacidg'being treated with an aqueous agent containing. these substances. The alkaliusedshould lbe of an alkali metal salt i. e. sodium, potassium, etc. which alkali is 6 preferably first made to react-withthe lignin soas to make the lignin water soluble the solution of thelignin andalka'li then being made to react with the fat. Preferably 0.1 to 0.5% lignin by weight of the weight of the fat is used. U

The mechanism of the-operation of the lignin ls'clear i'n that 'the lighin precipitates the protein and some nietalsalts aiong vithit. A brine solu tion 20% salt in water) "may be used to salt out thelignin wh'ich seern's to in-some way attach itself wlththe protein and other impurities in the rat. I The-precipitation f'these impurities by the lininfle ye'sfthfe rat-extremes pure and filtrable. The lig'nin "in do bination'yiith impurities is then filtered off in any normal manner leaving the purified r whe e im de iti n wea er melanin-alka when: "It he p be w andp'r'eierablyf bet n 5 and 6. Where Part a r li e 011 .b th ir th g fs i ed ere with c1 9W1? H m lk li u i a rwee n er. H .6

digninpsed asstatedabovesho ld be a ne ie lyr ri i fliwm uf h t 1 fil under the trade name Rinico 957.-

igi'iii'i has a low [ash content, lender 015 which ash content can be easily checked as a criterium for purity and constant quality. The acid character (pH 3 to 4) of these lignins permits the addition of alkali up to a desired pH which can be easily controlled according to the effect which should be produced in the various refining steps. The use of these inert qualities of the lignin in the refining and purification of the fats produces extremely unexpected and beneficial results.

If protein or lecithin removal from a vegetable or animal fat is intended in order to clarify a cloudy raw fat, the addition of alkali to the lignin is controlled so as to yield a pH no greater than 7. Preferably the pH is is done in order to avoid the formation of fatty acid soaps which will also contaminate the pro- It is of course preferred not teins and lecithins. to contaminate the proteins and lecithins since the proteins contained in the sludge layer are recoverable by acidification. Lignin being an inert material does not in any way impair the value of the protein when attached to it in some sort of protein-lignin attachment. This is one of the reasons why it is preferable to use a spe-' cially purified lignin such as Rimco 957. The proteins may be recovered from the excess water and separated from any entrained oil by acidification with phosphoric acid, monobasic sodium phosphate, citric acid, acetic acid etc. or any mixture of acids or acidic matters.

For partial neutralization of free fatty acids along with clarification of the contaminating proteins and lecithins, the alkalinity of the lignin-alkali solution is adjusted so as to be pH 7 or more. The pH should not be too high so as to avoid an attack on the neutral fat which invariably occurs when the conventional alkali refining procedures are used which employ excess alkali to facilitate separation of oil and soap stock. Lignin oil neutralization inactivates the excess alkali and separates the soap stocks formed from the clear oil by its higher specific gravity.

Lignin is also useful in the hydrogenation of a fat with a nickel catalyst, the lignin having an accelerating effect on hydrogenation with a nickel catalyst and allowing for better separation of nickel traces in the filtered hardened fat due to the inactivation of nickel-soaps which are usually formed in the course of hydrogenation using a nickel catalyst.

Lignin treatment is also useful in improving the bleachability of fats etc., the fats then being bleached to yield a much better bleached product. In this case the fat is treated with an aqueous agent containing an alkali such as sodium hydroxide or sodium phosphate and lignin, the treated fat then being separated from the precipitated impurities by i. e. filtration. This purified fat which requires no washing may then be bleached in any known manner to yield the well bleached fat.

Oil solvent mixture from the extraction of fatty tissues contains fines in suspension, i. e. protein particles which float throughout the miscella and give it a cloudy appearance which does not disappear by settling, centrifugation or filtration. The protein particles should be recovered, and if not separated prior to solvent distillation, ruins their feed value to some extent or cause burning i. e. discoloration of the oil and a rise in the content of free fatty acids. It has been found that the addition of clay or filter aids in a filtration step, still left the miscella cloudy and that the greater portion of the fines" had to be prekept between and 6. This following examples which disclose preferred em- 'bodiments of thepresent invention without, however limiting'the scope of the invention to the examples.

' Example I Clarification of freshly rendered tallow which is cloudy in appearance because of contained pro teinaceous matter may be accomplished as follows:

500 grams animal fat, unsettled, is mechanically stirred and heated to C. with 40 cc. water containing 1.5 grams lignin in the form of Rimco 957, 0.75 gram sodium hydroxide and 1.00 gram trisodium phosphate. To this mixture is added 50 cc. brine (20% salt solution) the mixture is then stirred and heated up to between 75 and 85 C. for 10 to 30 minutes and then allowed to settle for 10 minutes. The resulting fat is clear and filterable.

Example If I Another example of clarification of freshly rendered tallow is the following: 7

500 grams of the same unsettled fat as in Example I is simultaneously stirred and warmed by live, wet steam until it reaches a temperature of about 85 C. This heated fat is then sprayed, without stirring, with a hot water solution containing 5% lignin (Rimco 957), 2% sodium hydroxide and 3% trisodium phosphate until the cloudy oil appearance starts to clear. Hot brine spray follows to complete the initiated clarification. The sludge settles immediately.

In this example after the sludge settles and after removal of the bottom portions, the decanted clear oil may be filtered but is practically clean and moisture free even without filtration.

The proteins contained in the sludge layers of the two examples could be recovered by acidification with prosphoric acid, monobasic sodium phosphate, citric and acetic acid, or preferably a mixture of the acidic matters which breaksthe filtrable protein-y-lignin from the excess water and any entrained oil.

Trisodium phosphate and brine washing of animal fat is not new, but the effect of these ingredients without theaddition of lignin is much slower, requires additional water washing and long settling steps which always cause free fatty acid uptake and do not permit protein recovery.

Emample III Partial neutralization of fat may be carried out as follows:

500 grams protein-free fat of clear appearance and having FAC color of 23-25 and a free fatty acid content of 11.5% is heated up to 85 C. FAC color refers to standards of color set up by the Fatty Acid Commission, according to the standards of the American Chemical Society and the American Oil Chemical Society, the most desired product having the lowest color.

This heated fat is then sprayed without agitation with 50 cc. of a hot water solution containing 0.75 g. lignin (Rimco 957) 0.50 g. trisodium phosphate and 2.00 g. sodium hydroxide. To this is then added 50 cc. of brine.

The soap stock thus formed settles fast and sharp and the clean, clear oil layer tests 8% residual free fatty acid and a FAQ color of 19. This FAC color makes the clean tallow acceptable by the Fatty Acid Commission as a special tallow, and is without fixed or masked color body and free from soap or alkali traces.

Conventional partial neutralization would cause a breakdown in the oil composition. This is true because a fat containing such high proportion of free fatty acids is unstable due to the free fatty acids autocatalyzing the production of additional free fatty acids from the fat in the presence of impurities. Free fatty acids are liable to reform new free fatty acids from the breakdown of monoand di-glycerides formed by the alkali attack on the oil structure, also causing glycerin loss. Partial'neutralization carried out in the conventional manner is characterized by unseparable flowing soap stock particles which do not settle or wash down. If lignin is used as a soap stock carrier no floating unseparable soap traces remain in the partially neutralized oil.

Example IV Removal of oil soluble metal soaps and iron may be accomplished as follows:

500 grams of substantially protein-free fat from Example I or II above is washed with 150 cc. of water solution containing 0.6 grams sodium phosphate monobasic 0.5 grams phosphoric acid 0.30 grams oxalic acid 0.30 grams citric acid 0.15 grams acetic acid the solution being at about 85 C. This precipitates all of the oil soluble metal soaps and iron which may then be separated by filtration.

If the ash content of a fat is particularly low or if thework is carried out in large size operations (60,000 lbs. per batch) the total amount of the acid mixture is not over 0.1% based on the weight of the oil. The synergistic action of the said combinationmakes it possible to Work with such minute amounts of acids to precipitate the oil soluble impurities without any attack on the oil structure, as does occur when sulfuric or hydrochloric acid would be used for a similar purpose or when e. g. phosphoric acid by itself in sufficient strength would be. used. The action of the above acid wash is instantaneous and the separation of the acid Water is quite sharp without any emulsion layer. The color of the'oil is hardly changed after such a wash but the bleachability is now fully-established since no oil soluble soaps interfere with the action of ableaching clay or oxidation bleach.

This acid wash greatly improves the bleachability of the fat.

Dark colored industrial fats having an F'AC color 37-45, unbleachable in up to 10% clay or carbon treatments or by oxidationwith chlorine dioxide yield an FAC color of 19 when acid washed asabove, prior to bleaching. This acid wash by freeing from the fat the oil soluble metal soaps, yields low color readings, in the bleaching step which are impossible to obtain otherwise.

Fats which are. bleached before a: treatment with lignin as in Examples I, II, IIIorIV do not yield. asgood a product as fats bleached after treatment with lignin. Raw fats which are bleached with bleaching clay or carbon mixtures, up to 10% of bleaching powder by Weight of the Weight of the fat, or with chlorine dioxide gas produce at best an F'AC color 21.

19 PAC fat obtainedfrom raw fats with an FAC color 23-25 which are treated with lignin as in Examples I, II, III, or IV give an FAG color of 5-7 (fancy tallow grade). Furthermore there is a marked deodorization effect on the pretreated and then bleached tallows as against conventionally bleached fats.

.It is also possible to improve the bleachabality of low protein containing fat by a simplified lignin Wash.

Example V 450 grams of untreated industrial tallow is heated up to approximately C. To this is added 1.5 g. lignin (Rimco 957) slurried in 10 cc. water which is mixed with 10 cc. of Water containing 0.75 g. sodium hydroxide dissolved therein. This is heated for 15 minutes and then left to settle for 15 minutes. The settled fat which requires no washing is treated with 3% special Filtrol and the fatis found to have an FAC color of 1-3.

Industrial tallow, with the color of 19 PAC treated with 3% special Filtrol in a conventional manner by contacting with activated commercial clay and then filtered had an FAC color of 5-7. A comparison of this with lignln treated tallow clearly shows the improvements by the use of lignin.

It is well known that sodium hydroxide can be used to wash out color from a fat which still has loose i. e. unfixed and not burned-in, color particles. However, soap traces left from a conventional hydroxide wash are very difficult to remove, are time and oil wasting, and give cause to foaming and inactivation of bleaching clay as well as filtration difficulties. Therefore a sodium hydroxide treatment prior to clay bleaching cannot be practically applied.

In combination with lignin, the sodium hydroxide has hardly any alkali reaction when used in the indicated proportion, therefore practically preventing the formation of any free fatty acid soaps. Impurities are thus washed out andno after wash is required. Furthermore the settled oils do not foam or froth when reheated and brought into contact with bleaching clay at elevated temperatures. Filtration occurs rapidly and cleanly when the bleaching clay is most efficiently used in the absence of impurities, this being clearly shown by the dilference in the lighter color range achieved.

Example VI Miscella oil clarification may be carried out as follows: I

400 cc. of tallow miscella containing approximately 15% fat is mixed at about 40-60 C. with 10 cc. of water containing 1.5 g. lignin (Rimco 957), 0.75 g. sodium hydroxide and 0.25 g. lime.

Settling and clarification proceeds immediately and after removal of the sludge portion the clarified product is sprayed with 10 cc. of water containing 0.5 g. citric acid to break any metal soap emulsion.

After the clarification of a .miscella the distillation of solvent does not endanger the color of the raw fatand proceedsfaster. and smoother in the absence of fines. Of course a partial neutralization of the free fatty acids in the presence of lignin can be effected on the miscella oil and if this is followed with bleaching and filtration using preferably spent clay, in fresh non-oxidized state, the miscella benefits in color without contamination by mineral acid traces contained in new bleaching clay. Light colored oils with a low free fatty acid content and free from customary fixed impurities are formed and subsequent refining steps are greatly facilitated.

Facilitation of neutralization in the presence of lignin is proven by the following test:

(a) 500 grams ricebran oil with a free fatty acid content of 0.53% was mixed with cc. of water containing 0.5 g. sodium hydroxide, agitated and heated to 140 F. and then settled. The topped oil had a free fatty acid content of 0.12%. Refining of this caused a refining loss of 5.8%.

(b) 500 grams ricebran oil mixed with 2.5 grams lignin and 10 cc. of water containing 0.5 gram sodium hydroxide was agitated and heated to 140 F. and then settled. The topped oil has a free fatty acid content of 0.12% but refining caused a refining loss of only 1.4%.

Example VII The use of Rimco also aids in the hydrogenation of oils and other fats. may be carried out as follows:

500 grams cottonseed oil, salad oil quality was mixed with 10 grams Rufert nickel catalyst, 2 grams Hyflo Supercel, filter aid and 2 grams lignin (Rimco 957). drogenated in 30 minutes to an iodine value of 15. It filtered extremely clear and free from hydrogenation odor.

Another sample treated exactly as above however, without the use of lignin and hardened under exactly the same conditions reached an iodine value of 20 in the same reaction. Furthermore it filtered less clear, somewhat colloidal and with a normally noticeable hydrogenation odor.

The removal of metal soaps and iron from fat is greatly facilitated by pre-treatment with lignin but does however still require difficult removal operations. The removal of these impurities is greatly facilitated by the use of and treatment with phosphoric acid and/or sodium phosphate so as to separate the metal soaps and further or simultaneous treatment with at least one organic acid such as oxalic acid, citric acid, or acetic acid which precipitates iron traces.

In accordance with a preferred embodiment, this refining treatment is combined with the step of subjecting the thus treated substance to treatment with a small percentag of at least one organic acid adapted to precipitate traces of iron contained in the substance, and removing thereafter the thus precipitated iron traces.

It has been found also of advantage to subject before the above described treatments the fat, wax or fatty acid to a heat treatment, e. g. by subjecting an intimate mixture of this fat, wax or fatty acid and a small percentage of a finely divided metal catalyst to pressure at an elevated temperature. I preferably mix the fat, wax, or fatty acid to be purified with a small percentage of a spent metal catalyst, e. g. a spent nickel or nickel-copper catalyst, and then subject the thus obtained mixture to hydrogen pressure at temperature above 212 F., preferably at a temperature slightly above 212 F.

Such hydrogenation This cottonseed oil hy- It has been found that addition of the spent catalyst in combination with subjecting the mixture to hydrogen pressure at a temperature slightly above 212 F. produces the required bleaching and purifying effects within a surprisingly short time without the necessity of raising the temperature during this process to one which is not advisable in the ordinary steel vessels customarily used. Furthermore, it has been found that this new pretreatment makes it possible to substantially decrease the amount of activated catalyst needed for the consecutive hydrogenation, thereby making hydrogenation of such substances possible which up to now could not be economically hydrogenated because of the high costs caused by the relatively large amounts of catalyst needed therefor.

It is advantageous to use a hydrogen pressure of between 50 and 750 pounds and to agitate the mixture while it is under this pressure and at a temperature of about 220 to 225 F. I have also found it advantageous to add to the mixture before the hydrogen pressure and heat treatment a small percentage of a bleaching agent, e. g. from one percent to five percent of activated earth and about one percent of activated carbon. Addition of these agents substantially decreases the amount of formed nickel or other metal soaps so that removal of these soaps by consecutive treatments will be either entirely unnecessary or substantially facilitated.

Of course, the percentages of the bleachin and purifying ingredients used for the purposes of the present invention might be varied between relatively wide limit-s depending on the composition and characteristics of the treated materials. Thus, for instance, I have found that best results might be obtained in the process of purifying crude tall oil if the same is mixed with about one percent to five percent of activated earth, about one percent of activated carbon, and about two to five percent of spent metal catalysts, preferably spent nickel or nickel-copper catalysts. I may also add a small percentage, e. g. about one percent, of inactivated kieselguhr particularly of various filtercels, which addition serves as carrier for the impurities during precipitation, thereby facilitating removal of the same. I wish to note that if the spent catalyst used for my process contains already used filter material, no fresh filtercel, kieselguhr or activated carbon have to be added separately.

Of course, for refining and bleachingother fatty acids, the percentages of added agents have to be varied; thus, for instance, I have found that undistilled cotton oil fatty acid and undistilled oleic acid and similar acids may be refined by mixing them with about one percent to two percent of a spent catalyst, about one quarter of a percent to three quarters of a percent of activated earth, about one quarter to three quarters of a percent of filtercel, and about one quarter of a percent of activated carbon, and then treating the thus obtained mixture in the same way as explained above, with the only difference that a hydrogen pressure of not more than 50 pounds has to be applied.

The above described treatment of the undistilled fatty acids, as for instance tall oil, will result in substantial bleaching and refining of the acids; however, the same will still contain the metal soaps formed by the above described treatment with the spent catalyst. These metal soaps, particularly nickel and/or copper soaps, are then removed by a subsequent treatment with The thus hydrogenated fatty acids mightstill contain some traces of metal soaps, e. g. nickel and copper soaps; they might also contain colloidal nickel and/or copper impurities caused by the hydrogenation treatment; finally, they may also contain traces of iron if they were treated or rendered in iron vessels. To remove these metals and metal soaps, the hydrogenated fatty acids are again subjected to treatment with phosphoric acid and/or sodium phosphate which remove the metal soaps and the colloidal metals and with an organic acid, e. g. acetic, citric or oxalic acid, to remove the iron traces. This latter treatment might then finally be followed by subsequent bleaching with fullers earth and activated carbon.

I wish to stress that, as stated above, my present invention relates to processes of refining and purifying fats, for instance oils of vegetable origin, cotton seed oil, linseed oil and soybean oil and oils of animal origin, for instance whale oil, tallow, and hog fat; it also relates to refining and purifying of Waxes of animal origin as sperm oil, liver oils with a high content of unsaponifiables and mullet oil, of waxes of vegetable origin as jojoba oil, of mineral oils as liquid paraffin, and of mineral waxes as ozokerite, i. e. mixtures of hydrocarbons. My present invention furthermore relates to fatty acids and fatty matters of mixed compositions. Thus, the term fats, fatty acids and waxes as used above and in the following claims is intended to cover all substances and materials of the groups listed above.

Of course, also the term fatty acids used in the preceding description of my invention is to be understood as broadly as possible and the processes described above might be used also for and in connection with all above mentioned substances and materials.

Thus, for instance, this term is intended to include not only single fatty acids or other substances but also mixtures of such fatty acids and other substances, these mixtures might be purified or unpurified, distilled or undistilled; they might also contain other materials, as for instance, rosin acids or the like.

The following examples are illustrative of my process, although it is to be understood that I do not intend to limit myself particularly thereto:

Example A Neutralized, clear cocoanut oil is melted, mixed with 0.2% filtercel, 0.1% Raney catalyst and then hydrogenated under 50 pounds pressure p. s. i. at a maximum temperature of 300 F. The oil, practically completely hydrogenated to iodine val. 0.5 is filtered clear from the catalyst by the introduction of more filtercel to precoat the filter press. The warm oil is then mixed with 0.01% phosphoric acid and 0.1% sodium acid phosphate dissolved in warm Water and the whole is boiled up with open steam close to the boiling point of water, then settled for a short time. Greenish Water can be removed from the bottom of the kettle, after which the oil is sprayed with 1 136. hot caustic soda to remove all the free acidity calculated as lauric acid, the oil is washed soap free by hot water sprays and then filtered with 0.1% Hyfiosupercel and 0.05% charcoal (Nuchar GFO). The thus treated oil is perfectly water white and stays color stable and free from hydrogenation smell and taste ready for edible use without following steam deodorization.

Example B Neutralized and bleached soybean oil is mixed with 0.5% Rufert catalyst which has 25% nickel content, rest protection oil, 0.2% Hyfiosupercel, 0.05% Nuchar, neutral grade, then submitted to hydrogen under 50 pounds pressure p. s. i. at around 300 F. until shortening consistency or oleo margarine consistency has been achieved with a corresponding iodine value around 60. After careful filtration the oil is boiled up with 1% sodium silicate dissolved in twice its weight of water until a temperature close to water boiling has been reached. The settling yields a granulated soap and colored water at the, bottom of the kettle and the rest of the neutralized oil is washed with hot water. Then drying under vacuum follows and /2% of activated bleaching earth, together with 0.01% acetic acid and 0.01% citric acid are added to achieve a stable color of not more than 0.1 red, 2 yellow Lovibond. The fats are cooled before filtration on the filter press, under vacuum, and the filtered fat is then steam-vacuum deodorized and then remains without soybean fiavor reversion on a long in duction period.

Example 0 Crude tall oil is intimately mixed with five percent of activated earth, preferably Retrol, one percent of filtercel, i. e. inactivated kieselguhr, two percent of spent nickel-copper catalyst, and one percent of activated carbon. After these additions are finally divided in the tall oil, the temperature of this mixture is raised up to 200 F. and then hydrogen is introduced under pressure of about 250 pounds. Thereafter, the temperature of the mixture is further raised until 225" F. and then maintained at this level for about two hours. During this time, the mixture is agitated in order to obtain intimate contact of the oli with all added bleaching and refining agents and with the hydrogen introduced under pressure. 1

After maintaining hydrogen pressure for about two hours, the temperature of the oil is lowered and the thus treated oil filtered. Thereafter, the clear filtered oil is stirred in an open vessel and about 0.3% of phosphoric acid having a specific gravity of 1.041 and about 0.1% of monobasic sodium phosphate are added, both said substances well dissolved in water; the preheated oil together with these admixtures is then heated up to 200 F. and reacted with the acid and phosphate for at least thirty minutes.

The oil is then settled without stirring for at least thirty minutes and the precipitated greenish nickel and copper soaps are then removed. The thus obtained clear, substantially refined talloil might then be mixed with about 0.1% of filtercel and filtered.

If the thus cleaned tall oil is to be used as oil without any following hydrogenation, it can be once more treated with fullers earth and activated carbon. Previous to such treatment, 0.01% of an organic acid like acetic, citric or oxalic acid can be added to remove iron traces; this step will promote the bleaching effect of the subsequent bleaching treatment with fullers earth and activated carbon.

The preheated tall oil can then be hydrogenated. The process steps are similar to the customary ones; the main difference is that a mixed metal catalyst consisting of two thirds of nickel and one third of cooper is used and that not more than one percent of this catalyst is needed for obtaining excellent hydrogenation results.

1-3 Furthermore, the hydrogenation is carried out at about 225"F: under apressure of 750 pounds or somewhat less.

This hydrogenation treatment might be followed; by. purification of the hydrogenatedoil; in orderto remove formedlmetallsoaps, e. a nickel and; copper soaps, colloidal; nickel and copper; and; iron traces. This; is; obtained by repeated treatment. with about 0.5% of phosphoric; acid;- about; 0.2% of: sodium phosphate, followed: by subsequent treatment with about 002% Of? an organic acid. This latter step; might.- then; be followed; by subsequent. bleaching with, fullers earth and activated: carbon.

Estima D ll ist led d .11.1,- e c m erci l eic a d. s t ee d. n h same. way s de c ed n E??- mslalv to? cotton 0.11 fatty acid xampl F Undisti'lled crude tall oil is hydrogenated without any pretreatment with a mixed nickel-- copper catalyst consisting of two thirds oiniokel ant lone third of copper. The hydrogenation steps themselvesare identicalwith thoseof: other customary hydrogenation treatments. The only diif erenceisf that'by use of the above described new catalyst ood hydrogenation results might beobta ined also without any purifying pretreatment in case of certain types of crude tall oil while customary catalysts will not have any hydrogena tion: effects without pretreatment ofthe crude il} Erample G Crude. cottonseed oil, dark colored and still con? taining its original free fatty acid content is in: timately mixed with two percent of spent nickel:- copper catalyst and 1% 0t filtercel, inactivated k-ieselguhr. The temperature. of this mixture is raised up 130.200. F. and then hydrogen is. intro..- duced under pressuraof about 250lbs. This tem: perature is maintained for about twohours. Dur-. ing. this time, the mixture is. agitated in order to, obtain intimate contact of the oil and: its refi in reagent and with the ydroee keutueder e sure he tem e ature o em tut s hsn bw r d o ab 0 he att s te e ea ed and the thus treated oil filtered.

The oil is, now only caustic refined in the; customary way which gives, the advantage that th roo h obtain a e much. c eaner and m t lua l laQ qallfi i wash s are ttquir d obtain a clear, neutral oil, which results in decreased refining losses. The neutral oil, is refittered with filtercel and unactivated fullers earth to remove the last traces of -soap If the thus cleaned cottonseed oil is to be used as liquid oil, it can be treated once more with activated earth and carbons; Previous to such treatment, 001% 01' an organic acid like acetic or citric (not oxalic because it is toxic for edible oil purposes) can be-added to remove iron traces; this step will promote the bleaching eflect of the subsequent treatment with activated earth and carbons. The pretreated oil has better keeping qualities and can be deodorized in the regular way but under savings of steam.

The pretreated cottonseed oil can also be hydrogenated; The process steps are similar to the customary ones; the main difference is that a mix-ed metal catalyst consisting of of nickel and V oicopper is used and that a small percentage or thecatalyst can be roused much more often. Further-more, the hydrogenation is car ried out at about 225? F. under-a pressure of 250 lbs. or somewhat less.

This hydrogenation treatment might be followed by purification or the hydrogenated cottonseed oil'in order to remove formed metal soaps, e. g nickel and copper soaps, colloidal nickel and copper and iron traces. This is obtained by a treatment of 0.3% of phosphoric acid having a specific gravity o1 1.041 and about 0.1% of monobasic sodium phosphate which are both Well dissolved in water and added to the hydrogenated, filtered cottonseed oil The hydrogenated oil together with these admixtures is then kept under intimate stirring for at. least 30 minutes; the temperature is maintained around 180 F. but not less than 150- The oil is then settled without stirring for at least 30 minutes and the precipitated greenish nickel and copper soaps are then removed, The thus obtained clear hydrogenated cottonseed oil is mixed with about 0.1 or filtercel and filtered. The oil is then submitted to a short steamdeodorization under vacuum. Citric acid to remove iron traces (0.01%)

can be added in this step. The deodorized oil is ready for a first-class shortening with excellent stability and a-highsmoke point.

@rude, dark tallow, high in free. fatty acid is intimately: mixed with 73 spent catalyst and 4% of-filtercel, M 76 activated earth. The temperature. of this mixtureiisraised to 200 F. and then hydrogen. is introduced and kept at a pressure. of 50 lbs. This temperature is maintained for about two. hours. During this time, the mixture is agitated in order to obtain intimate contact of the oil and its refining reagents. and with the hydrogen kept" underpressure'. The temperature of the mixture is then lowered to about lithe pressure released andthe; thus treat- Bd oil: filtered.

The oil can be now caustic refined, totally or partially, in the. customary way. The neutralized tallow is refiltered with less than 4% of neutral earth to remove the lasttraces of soap in case a hydrogenation treatment follows for the purpose ot saturation ofthe double bonds and increase ol melting-point and titer.

If: the thus cleaned tallow is to be used as such without subsequent hydrogenation it can be treated once more with activated earth and carbons. Previous to suchtreatment, 0.01% of an organic acidlikeacetic or citric- (not oxalic, because it is toxic for edible oilpurposes) can be added t remove iron. traces; this step will promotethe bleachimg- 'effect-o1 the subsequent treatment with activated earth and carbons; The purified talloiu has: better keeping qualities of color and: odorand can be used for high class white, perfumed.toiletapreparations The pretreated tallow can also be hydrogenated. The process steps are similar to the customary ones; the main difference is that a mixed metal catalyst consisting of of nickel and of copper is used and that a small percentage of the catalyst can be roused much more often. Furthermore, the hydrogenation is carried out at about 225 F. under a pressure of 250 lbs. or somewhat less.

This hydrogenation treatment might be followed by purification of the hydrogenated tallow in order to remove formed metal soaps, e. g. nickel and copper soaps, colloidal nickel and copper and iron traces. This is obtained by a treatment of 0.3% of phosphoric acid having a specific gravity of 1.041 and about 0.1% of monobasic sodium phosphate which are both wel1 dissolved in water and added to the hydrogenated, filtered cottonseed oil. The hydrogenated oil together with these admixtures is then kept under intimate stirring for at least 30 minutes; the temperature is maintained around 180 F. (not less than 150 F.) The oil is then settled without stirring for at least 30 minutes and the precipitated greenish nickel and copper soaps are then removed. The thus obtained clear hy drogenated cottonseed oil is mixed with about 0.1% of filtercel and filtered.

Example I Crude jojoba oil is intimately mixed with spent catalyst, /i.% of filtercel, of carbon. The temperature of the mixture being raised to 200 F. and then hydrogen is introduced and kept at a pressure of 50 lbs. This temperature i maintained for about two hours. During this time the mixture is agitated in order to obtain intimate contact of the oil and its refining reagents and with the hydrogen kept under pressure. The temperature of the mixture is then lowered to about 180 F. and the pressure released and the thus treated oil filtered. Thereafter, the clear filtered oil is stirred in an open vessel and about 0.3% of phosphoric acid having a specific gravity of 1.041 are added, both said substances well dissolved in water; the pretreated oil together with these admixtures is then heated up to 200 F. and reacted with the acid and phosphate for at least 30 minutes. The oil is then settled without stirring for at least minutes and the precipitated greenish nickel or nickel-copper soaps are then removed. The thus clear and substantially refined jojoba oil might then be mixed with about 0.1% filtercel and filtered. The filtercakes of spent catalyst and filtercel from these two filtration steps cannot be reused again.

The pretreated oil is already light in color and does not require any further purifying step for the majority of cases where it might be used in the liquid form. The pretreated jojoba oil can also be hydrogenated. The process steps are similar to the customary ones; the main difference is that a mixed metal catalyst consisting of of nickel and of copper is used and that a small percentage of the catalyst can be used for even a complete saturation. Furthermore, the hydrogenation is carried out at about 225 F. under a pressure of 250 lbs. or somewhat less.

For the majority of purposes the thus'treated and filtered oil will not require any further washing, bleachin or deodorization treatments. The combined pretreatment with spent catalyst and the hydrogenation with nickel copper catalyst yield a color and odor free hard jojoba oil with- 16 out any further treatment which presents itself as a spermacetic-like crystalline wax.

Example J Crude dark mineral oil is intimately mixed with 5% of activated earth, preferably Retrol, one percent of filtercel, two percent of spent nickel or nickelcopper catalyst and one percent of activated carbon. After these additions are finely divided-in the oil, the temperature of the mixture is raised up to F. and hydrogen is introduced under pressure of about 750 lbs. The temperature of the mixture is kept under 200 F. for about 2 hours. During this time, the mixture is agitated in order to obtain intimate contact of the viscous mineral oil with all added bleaching and refining agents and with the hydrogen introduced under pressure. The thus treated oil is then filtered. The clear filtered oil is stirred in an open vessel and about 0.3% of phosphoric acid having a specific gravity of 1.041 and about 0.1% of monobasic sodium phosphate are added, both said substances well dissolved in water the pretreated oil together with these admixtures is then heated up to 200 F. and reacted with the acid and phosphate for at least 30 minutes. The mineral oil is settled without stirring for about 30 minutes and the precipitated greenish metal soaps are then removed. The thus obtained clear oil is greatly improved in color and odor and a test will show a sharp decrease in sulphur compounds. The oil is filtered with a small percentage of filtercel and then rebleached with fullers earth and activated carbon. Previous to such treatment, 0.01% of an organic acid, like acetic, citric and/or oxalic can be added to remove iron traces; this step will promote the bleaching effect of thesubsequent bleaching treatment with fullers earth and activated carbon.

It will be understood that each of the elements described above, or two or more together, may also find a useful application in other types of purification and refining steps differing from the types described above.

While the invention has been illustrated and described as embodied in purification and refining of fats, fatty acids and derivatives thereof, it is not intended to be limited to the details shown, since various modifications and structural changes may be made without departing in any way from the spirit of the present invenion.

Without further analysis, the foregoing will so fully reveal the gist of the present invention that others can by applying current knowledge readily adapt it for various applications without omitting features that, from the standpoint of prior art, fairly constitute essential characteristics of the generic or specific aspects of this invention, and, therefore, such adaptations should and are intended to be comprehended within the meaning and range of equivalence of the following claims.

What is claimed as new and desired to be secured by Letters Patent is:

1. Process of purifying and refining fats, and higher fatty acids, comprising the steps of treating a substance selected from the group consisting of fats, and higher fatty acids with at least one alkali metal derivative of a lignin so as to cause precipitation of the impurities contained in said treated substance; and separatin the purified product from the precipitated impurities.

i heating said said stirred hot mixture to stand .sisting of fats, and higher contained in 2. "-Process of it purifying and refining fats and higher fattyacids,"comprising the steps of mixing a substance selected from the group consisting of fats, and highcrfatty acids with -at-ileast one alkali metal derivative of a lignin so as to cause precipitation of impuirties contained in said treated substance; stirring said mixture; mixture While stirring; allowing so'as to settle; and separating the clear oil from the sludge in said settled mixture.

3. Process of purifying and refining fats, and higher fattyacids, comprising the steps of mixing a substance selected from the group *consisting of fats, and higher fatty'acids with at least one alkali :metal derivative of a 'lignin so as to cause precipitation-of impurities contained in said treated substance stirring said mixture; beating .said .mixture .while stirring; allowing said stirred hot mixtureto =standso as to settle; andfiltering the settled mixture so as to separate'the clear oil from thesludge.

4. Process of purifying and refinlng fatsjand higher fatty'aoids,comprising the steps of mixing a substance selected from sisting of fats, and higher "fatty aci'ds with an aqueous agent containing lignin and sodium phosphate so as to form *a sodium lignin'which acts on said substance to cause precipitation of impurities contained in said treated substance; stirringsaid mixture; heating said mixture while stirring; allowing said stirred hot mixture to stand so as to settle; and separating clear oil from the sludge in said settled mixture.

5. Processof purifying and refining fats, and ..1

higher fatty acids, comprising the steps of treat ing a substance selected from the group con sisting of fats, and higher fatty acidsy/ith an aqueous agent containing ligninand at least one alkali metal-compound so as to cause precipitation of the impurities contained in said treated substance; and separating the purified product from the precipitated impurities.

"6. Process of purifying and refiningfats, and higher fatty acids, comprising thesteps of treating a substance selected from the group confatty acids with an aqueous agent containing 0.1 to 0.5% by weight of the weight of the substance-being treated of lignin and at least one alkali metal compound so as to cause precipitation of the impurities said treated substance; and separating the purified product from the precipi tated impurities.

'7..Process of purifying and refining :fats, and

higher fatty acids, comprisingthe steps .of treat ing a substance selected from the group consisting of fats, and higher fatty acids with "a hot water solution containing lignin and at least one alkali metal compound, said alkali metal compound and said lignin forming in solution an alkali metal lignin which causes precipitation of the impurities contained in said treated substance; and separating the purified product from the precipitated impurities.

8. Process of purifying and refining fats, and higher fatty acids, comprising the steps of treating a substance selected from the "cup consisting of fats, and higher fatty acids with a hot water solution at a temperature above 60 ing lignin and at least one alkali metal compound, said alkali metal compound and said lignin forming in solution an alkali metal lignin which causes precipitation of the impurities contained in said treated substance; and separating the group con- 3 C. contain- :said mixture above 75 the :purifie'diproduct fromzthe precipitated Timpurities.

=9. Process.:of purifying :andjrefining fats, and higher fatty "acids, comprising the ing a substance selected from the group consisting of fats, and higher :fatty acids with 2. not aqueous agentcontaininglignin and at least one alkali metal'compound. so aswto cause precipitation of the impurities contained in said treated substance; stirring said mixture; heating C. While stirring; allowing said stirred hot mixture to stand so to settle; and separating the clear oil from the sludge in settled mixture.

10. Process of purifying and refining fatsyand higher fatty acids,- comprising the steps of mixing a substancesselected from the groupiconsisting of fats, and higher fatty acids with a :hot aqueous agent containing ligninand at least one alkali metal compound so as tenants precipitation of the impuritiescontained in said treated substance; stirring said mixture; heating said mixture above 75 C. for 10 to 30 minutes while stirring; allowing said stirred hot mixture to stand so as to settle; and separating the clear oil from the sludge in said settled mixture.

11. In a process of purifying and refining fats, and higher fatty acids, the steps of clarification comprising mixing a substance selected from the group consisting of fats, and higher fatty acids with an aqueous agent containing lignin and at least one alkali metal compound and being at a below 7 adapted to cause precipitation of the protein impurities contained in said treated substance; adding a brinesolution to said mixture; and separating the clarified substance from the protein-containing impurities.

12. In a process of purifying and refining fats, and higher fatty acids, "the steps of clarification comprising mixing a substance selected from the group consisting of fats, and higher fatty acids with an aqueous agent containing lignin and at least onealkalimetal compound and being at a pH between 5 and 6 adapted to cause precipitation of the protein impurities contained in said treated substance; adding a brine solution to said mixture; and separatingthe clarified substance from the protein-containing impurities.

13. In a process of purifying and refining fats. and higherfatty acids, the steps of clarification comprising mixing a substance selected from the group consisting of fatsyand higher fatty acids with an aqueous agent containing about 0.1 to 0.5% by weight of the weight of the sub stance being treated of lignin and at least one alkali metal compound and being at a pH below 7 adapted to cause precipitation of the protein impurities contained in said treated substance; adding a brine solution to said mixture; and separating the clarified substance from the pro-- tein-containing impurities.

14. In a process of purifying and refining fats, and higher fatty acids, the steps of clarification and partial neutralization, comprising mixing a substance selected from the group consisting of fats, and higher fatty acids with an aqueous agent containing lignin and at least one alkali metal compound and being at a pH above 7 adapted to cause precipitation of the protein impurities contained in said treated substance and to cause partial neutralization thereof; adding a brine solution to said mixture; and separating the clarified, partially neutralized substance from the protein-containing impurities.

15. In a process of purifying and refining fats, and higher fatty acids, the steps of clarification and partial neutralization, comprising mixing a v substance selected from the group consisting of vto said mixture; and separating the clarified,

partially neutralized substance from the protein containing impurities.

16. In a process of purifying and refining fats, and higher fatty acids, the steps of clarification and bleaching comprising mixing a substance selected from the group consisting of fats, and higher fatty acids with an aqueous agent containing lignin and at least one alkali metal compound and being at a pH below 7 adapted to cause precipitation of the protein impurities contained in said treated substance; adding a brine solution to said mixture; separating the clarified substance from the protein-containing impuri ties; treating said clarified substantially proteinfree product with at least one bleaching agent at elevated temperatures; and filtering said treated product so as to remove the bleaching clay thereby obtaining a pure, clarified, bleached product.

17. In a process of purifying and refining fats, and higher fatty acids the steps of miscella oil clarification comprising mixing a miscella de rived from a substance selected from the group consisting of fats, and higher fatty acids with an aqueous agent containing lignin, at least one alkali metal compound and lime and being at a pH below 7 so as to cause precipitation of pro tein particles contained in said miscella; and separating the clarified product from the me cipitated protein-containing impurities.

18. Process of purifying and refining fats, and higher fatty acids, comprising the steps 01- mix ing a substance selected from the group consisting of fats, and higher fatty acids with an aqueous agent containing lignin and sodium phosphate so as to cause precipitation of im purities contained in said treated substance; stirring said mixture; heating said mixture while stirring; allowing said stirred hot mixture to stand so as to settle; separating the clear oil from the sludge in said settled mixture; subjecting the thus treated substance to treatment with a small percentage of at least one organic acid selected from the group consisting of oxalic acid, citric acid and acetic acid so as to precipitate the traces of iron contained in said substance; and removing the thus precipitated traces of iron thereby recovering a product substantially free of metal soaps and iron.

19. In a process of purifying and refining fats, and higher fatty acids, the steps of hydrogenation comprising mixing a substance selected from the group consisting of fats, and higher fatty acids with a nickel catalyst and lignin; treating said mixture with hydrogen so as to hydrogenate the substance being treated; and filtering said mixture so as to separate the hydrogenated substance from nickel and lignin thereby obtaining a clear highly hydrogenated product.

20. Process of purifying and refining fats, and higher fatty acids, comprising the steps of mixing a substance selected from the group consisting of fats, and higher fatty acids with an aqueous agent containing at least one watersoluble alkali metal compound and a lignin which react in the water to form a soluble alkali metal lignin, said alkali metal lignin causing precipitation of impurities from said substance; stirring said mixture; heating said mixture whie stirring; allowing said stirred hot mixture to stand so as to settle; and separating the clear oil from the sludge in said settled mixture.

21. Process of purifying and refining fats, and higher fatty acids, comprising the steps of mixing a substance selected from the group consisting of fats, and higher fatty acids with an aqueous agent containing at least one water-soluble alkali metal compound selected from the group consisting of sodium hydroxide and sodium phosphate and a lignin which react in the water to form a soluble alkali metal lignin, said alkali metal lignin causing precipitation of impurities from said substance; stirring said mixture; heating said mixture while stirring; allowing said stirred hot mixture to stand so as to settle; and separating the clear oil from the sludge in said settled mixture.

ILONA TAUSSKY.

References Cited in the file of this patent UNITED STATES PATENTS Pamphlet published by The Mead Corporation, Research and Development Department, Chillicothe, Ohio. 

19. IN A PROCESS OF PURIFYING AND REFINING FATS, AND HIGHER FATTY ACIDS, THE STEPS OF HYDROGENATION COMPRISING MIXING A SUBSTANCE SELECTED FROM THE GROUP CONSISTING OF FATS, AND HIGHER FATTY ACIDS WITH A NICKEL CATALYST AND LIGNIN; TREATING SAID MIXTURE WITH HYDROGEN SO AS TO HYDROGENATE THE SUBSTANCE BEING TREATED; AND FILTERING SAID MIXTURE SO AS TO SEPARATE THE HYDROGENATED SUBSTANCE FROM NICKEL AND LIGNIN THEREBY OBTAINING A CLEAR HIGHLY HYDROGENATED PRODUCT. 